Catalytic reconstruction of hydrocarbons



March 25, 1947. F E, FREY 2,418,023

CATALYTIG `RECONsTRUc'xzIoN 0F HYDRocARBoNs Fmeduovfze, 1943 I Arm NEYs Patented Merli 25, 1947 UNITED STATE CATALYTIC RECONSTRUCTION F HYDROCABBQNS Frederick E.Frey, Bartlesville, Okla., assigner to Phillips Petroleum Company, a corporation of Delaware Application November 26, 1943, Serial No. 511,871

' (o1. aso-esas) 21 Claims.

This invention relates to a catalytic process for reconstructing hydrocarbons. More particularly, it relates to the use of free, or elementary, hydrogen to modify and direct catalytic reconstruction c reactions of aliphatic hydrocarbons and/orto aid in regenerating hydrofluoric acid-containing catalysts used for such reactions. This application is a continuation-impart of my copending application Serial No. 426,627, led 'January 13, 1942, now U. S. Patent 2,403,649, issued July 9, 1946, and of my copending application Serial No. 460,867, filed October 5, 1942.

The rst of the aforementionedcopending applications discloses that in the presence of substantial proportions of hydrofluoric acid and under suitable conditions of timerand temperature saturated hydrocarbons are reconstructed to hydrocarbons of diierent carbon-skeleton arrangement and different boiling point. Parafflnic hydrocarbons, for example, undergo conversion to isomers and to hydrocarbons of both lower and higher molecular weights and correspondingly lower and higher boiling temperatures. In the second copending application I have disclosed that a marked improvement in the efficiency and utility of concentrated hydrouoric acid as a catalyst for reconstructing hydrocarbons is brought about by including with it a minor proportion of boron fluoride. I have now found that inthe presence of lcatalysts which comprise hydrofluoric acid, with or without minor added proportions of boron iiuoride, elementary hydrogen may react with aliphatic hydrocarbons; that'elementary hydrogen has adirecting influence on reconstructing reactions; that the presence of elementary hydrogen in reconstructing reactions increases the life of the catalyst; and that the presence of elementary hydrogen in steps for regenerating cat v alysts used for `the reactions increases the efficiency `of regeneration, especially of boron fluo,-

ride-containing catalysts.

It appears that, when hydrocarbons are subjected to conversion conditions in the presence of concentrated hydroiluoric acid as the essential or effective conversion catalyst, a number of reactions take place concurrently. When aparaflin hydrocarbon, alone, is converted the principal re- A actions are- (l) simple isomerization and (2) an isoversion, or the formation of paraflins both of higher and of lower molecular weights. These Reaction 2 will proceed with either normal pentane or isopentane, and the major amounts oi the products Willhave -a branched-chain structure. This reaction appears to be in somewhat marked contrast with reactions which take place in the presence of aluminum chloride. Although some isobutane can be produced from higher boiling paraflins in the presence of aluminum chloride, there does not appear to be so marked a formation of paraiiins having molecular weights immediately higher than the paraiiln reacted. Apparently the material which forms such parafflns when hydroiiuoric acid is the catalyst is degraded to a sludge with aluminum chloride.

Oleiin hydrocarbons also undergo various reactions, including one of naphthene formation. Likewise, cycloparain hydrocarbons undergo isomerization under similar conditions.

(3) CHaCrH CsHu (Methylcyclopentane) (Cycloliexane) I have now found that, when free, or elemen tary, hydrogen is present in appreciable amounts, these reactions are affected in different degrees,

`so that by controlling the amount of hydrogen verted appears to decrease somewhat, so that at the higher hydrogen pressures somewhat more drastic reaction conditionsare necessary in order to obtain the same extent of conversion of the hydrocarbon charge l-stock. The decrease in reaction rate ofthe hydrocarbons charged continues as the hydrogen pressure is further` increased, but another effect also cornes in; the hydrogen actively enters into the reactions so that none of the original reactions is predominant but rather reactions involving a consumption of hydrogen appear. In the case of paraffin hydrocarbons there is some indication that the various reactions taking place result in products which can be represented, generally, inthe following:

(Heptane) (Iso- (Iso- (Isobutane) pentane) hexane) In any event, paraffin hydrocarbons,` either straightor branched-chain are converted to other paraiiins which have lower molecular weights (and which are primarily branchedchain) and hydrogenis consumed.

When converting olefins in the pre'sence of hydrogen, under high hydrogen pressures, an additional reaction involving addition of hydrogen to an olenic linkage is involved. Thus, generally stated:

(Normal butene) (Isobutane) It is to be understood, of course, that the foregoing is a very general and theoretical discussion, and represents an attempt to explain, at least in part, the actual results which have been observed. It will be readily appreciated from the factual data presented hereinafter, thatY the actual reactions involved are not as simple, in all cases, as the general equations just presented.

As'previously mentioned, the presence of hydrogen makes it necessary to have somewhat more drastic reaction conditions in order that the hy- 'drocarbon charge will undergo conversion to the same extent.4 With a catalyst comprising solely hydrofluoric acid, or comprising hydrofluoric acid and a minor amount of boron trifluoride in fixed amounts, more drastic reaction conditions include higher temperatures and/or v longer reaction times. With other conditions fixed, the addition of boron trifluoride vto hydrofluoric acid, or an increase in its concentration, has a similar effect as an increase in reaction temperature and/or time, at least within ranges elsewhere herein discussed. However, it is not necessary, or desirable, to have the catalyst contain lmore than 8 to 10 per cent by weight of boron triiiuoride,and an amount less than 8 per cent will generally be found to be satisfactory. i

'I'he present invention, in aspeciflc embodiment, is directed primarily to the conversion of hydrocarbons in the presence of concentrated hydrofluoric acid as the effective or essential catalyst (either without or, and preferably, with boron triuoride as discussed) in the presence of a sumcient amount of free hydrogen to enable the hydrogenl to take part in the reaction and be consumed to an appreciable extent. Although, as is the case in connection with almost any other factor in chemical reactions, the differences between the effect of low hydrogen concentration and high hydrogen concentration have a tendency to merge from one to the other, it appears that a rather marked change occurs in the neighborhood of about 200 pounds per square inch of hydrogen pressure; above this pressure the hydroto any marked extent. This latter feature is dis-l closed more thoroughly, and claimed, in my copending application Serial No. 511,872, filed November 26, 1943.

An object of this invention is to increase the yield of low-boiling hydrocarbons obtained in catalytic reconstruction processes. A specic object of this invention is to provide a process for converting normal pentane to isobutane in high yield, Another object of this invention is to increase the life of catalysts which comprise hydroiiuoric acid and a minor proportion of boron fluoride. Another object of lthis invention is to increase the saturation of normally liquid gasoline-range hydrocarbons, such as are obtained from cracking processes. Other objects and advantages of the invention will become apparent. to one skilled in the art, from the following discussion and disclosure.

The present invention, broadly, .comprises treating petroleum hydrocarbons with hydrogen in the presence of a catalyst which comprises concentrated, or substantially anhydrous, hydrofluoric acid as the major or even as the sole component, Preferably, however, a minor proportion of boron fluoride such as not in excess of about 8 or 10 per cent by Weight, is included inl the catalyst to increase its activity and to enable the reactions to proceed rapidly at relatively low temperatures. Preferably also, in order to aid and accelerate the reaction of hydrogen, a minor proportion of a hydrogen carrier such as a salt or halide of Cr, Sn, Cu, Ni, Co, Fe, Cd, Zi, Mo, V, or Pb, may` be incorporated in the catalyst. One modification of the invention further comprises the step of heating spent or partially spent catalyst in the presence of hydrogen to regenera-te active hydrofluoric acid and boron fluoride. In one specific embodiment of my invention which is particularly useful, a low boiling normally liquid hydrocarbon such as normal pen-- tane, lsopentane, or normal hexane is treated with hydrogen in the presence of hydrofluoric acid to which has been added a minor proportion of boron fluoride to produce relatively lower boil ing hydrocarbons, particularly isobutane, as the major product. Another v ery useful embodiment o'f my invention comprises treating a mixture of saturated and unsaturated hydrocarbons boiling in the gasoline and/or kerosene range with hydrogen in the presence of concentrated hydrofluoric acid with or without catalyst modifiers,

' whereby complete saturation of the hydrocarbon gen tends to become one of the definite reactants mixture is attained without the loss of yield or volatility, resulting from alkylation, polymerization, etc., that may occur upon treatment with hydrofluoric acid in the absence ofv hydrogen. In-

deed treatment in the presence of hydrogen in y accordance with the principles of this invention 60" may be used to eii'ect an increase in volatility of such hydrocarbon materials.

In the practice of the invention isobutane is formed in much larger proportions than any other product and under controlled conditions may be obtained in ultimate yields of 60 mol per cent or more from hydrocarbons such as normal pentane, normal hexane, normal heptane, and/or isomers of these hydrocarbons. Normal butane may be isomerized to isobutane in the presence of elementary hydrogen and hydrofluoric acid to which a minor proportion of boron fluoride has been added. In isomerizlng normalbutane to isobutane, the presence of hydrogen does not appear to increase the ultimate yield of lsothecatalyst appreciably. It is also possible to obta-in appreciable yields of isomers of other hy-l stantially anhydrous hydroiluoric acid to which a minor proportion of boron fluoride has been added. It should be clearly understood, however, that the invention is applicable to other normally liquid saturated hydrocarbons and to oleflns, and that it is especially useful for converting normal paranlns, which are of relatively y low value, to isoparaillns, which are useful in the production of motor fuel ingredients having' high antiknock ratings.

Normal pentane is admitted through inlet II to reactor I2, wherein it is agitated with concentrated hydrofluorlc acid to which has been added a minor proportion of boron fluoride, which may be admitted through inlet I3, and hydrogen, which may be admitted through inlet Il. The proportion of boron fluoride may be in the range of about 1 to about 30 per cent by weight per cent is highly satisfactory. A proportion in the range of about 1 to 5 per cent is usually preferred because such a composition is a very active hydrocarbon conversion catalyst at 50 to 350 F., yet the proportion of added boron fluoride is suillciently low that the `cost of replacing and/or regenerating the catalyst is not excessive. In general the proportion of boron fluoride may be correlated with the reaction temperature, the optimum proportion being somewhat higher with lower temperatures. In many instances it is desirable to add small amounts of boron fluoride at various times throughout the course of the reaction, as at a plurality of points along the length of a long reaction zone through which a stream of reactants is continuously passed. The catalyst may be completely anhydrous, or a small proportion of water can be present. The relative proportions of catalyst and hydrocarbon maintained in the intermingled condition in the zone of reaction are, within a wide range, not critical. with hydrocarbon-catalyst ratios in the range of about 0.1:1 to 3:1 by weight, or more, and optimum results are obtained with ratios in the range of about 0.5:1 to 1.5:*1. The reaction conditions should generally be such that the hydro. fiuoric acid catalyst is present in the reaction zone as a liquid.

lThe reaction temperature for converting normal pentane may be in the range of about 50 to 600 F. and preferably inthe range of about Good results are obtainedv panyine 1o treated. A slightly higher temperature is required for ispentane and/or normal hexane than for normal pentane; the temperatures used for treating conversion stock containing olefins may be somewhat lower than those used for treating parafllns. Generally the time and temperature should be so correlated as to give at least about to 50 per cent conversion per pass. If one is willing to accept a somewhat inferior product, that is, one which contains small proportions of propane or the like, the reaction may be carried out with conversions as high as 80 per cent per pass or more. The exact optimum conditions may be readily determinedby trial for individual instances. drocarbons are only slightly soluble in one another, especially at relatively low temperatures, it is desirable to provide a means of agitation in reactor I2, so that the hydrocarbons and catalyst are intimately admixed. The means for agitation may consist of stirrers, jet inlets, or bames, or the reactor may bein the f orm of a I tube of such dimensions that the iiow of :reaction of the hydroiiuoric acid; usually, less than about mixture in it is turbulent. Rapid recirculation in a closed cycle with continuous introduction of charge and withdrawal of eilluents mayl also be practiced.

The partial pressure of hydrogen in the reaction zone may be varied over a wide range, such as about l0 to about,5000 p. s. i., or more; preferably, in order to effect the hydrogenolysis, or hydroverjsion, which is an object of this invention, it should be at least about 200 p. s. i., and preferably 500 to 2000 p. s. i.

After a suitable time in reactor I2, the reaction mixture is passed through conduit I5 to separator I6, wherein Aby cooling and gravitational or centrifugal means it is separated into three phases. Gaseous hydrogen may be bled off from the top of separator I6 through conduit I1 and `returned via conduit I8 to reactor I2. A liquid 100 to 350 F. A t such temperatures the reaction time, inversely dependent upon the temperature, may be in the range of about 5 minutes to several hours or more, but up to approrimately 2 hours will generally be sulcient. In general, the optimum reaction temperature and time dehydrocarbon phase is passed through conduit I9 to fractionator 20, wherein hydrogen is separated out by fractionation and is then returned through line I8 to reactor I2. If desired, light gases passed from iractionator 20 may be discharged, at least in part, through conduit I8A. Hydrocarbons from the kettle of fractionator 20 pass through conduit 2I to debutanizer 22. From debutanizer 22 a major overhead fraction, comprising principally isobutane with small amounts of hydroiluoric acid and sometimes propane, is passed through conduit 23 to separator 214, wherein it is separated into two liquid phases, The lighter or isobutane phase may be withdrawn through conduit 2-5. This isobutane is suiliciently pure for use as feed to an alkylation process; however, if desired it may be made substantially completely free of hydrogen uoride by passing it over bauxite at an elevated temperature, by further distillation, by washing with an alkali, or the like, and/or it may be separated from hydrocarbon impurities by distillation, in steps not shown in the drawing. The heavier or hydroiluoric acid phase from separator 24, which is relatively minor in amount, is returned through conduit 26 to separator I6. The kettle fraction from debutanizer 22 comprises `isopentane, unreacted normal pentane and small proportions of other hydrocarbons. This fraction is passed through conduit 21 to deisopentanizer 28 wherefrom isopentane may be withdrawn through outlet 29, and unreacted normal pentane and higher boiling hydrocarbons may be recycled through conduit pend upon the hydrocarbon material being 30 to reactor I2. If desired, this fraction may be As the catalysts and the reactant hyananas first subjected to additional fractionation steps for recovering relatively high boiling` isoparamns such as isohexane and isoheptane. In some instances, it may be desirable to provide an additional fractionator, not shown in the drawing. to remove small proportions of normal butane. When adequate quantities of isopentane are available from other sources, it wlllbe desirable to recycle the total kettle fractionfrom debutanizer 22 directly through conduits 3| and 30 to reactor I2; by this procedure isopentane\re acts further to increase the ultimate yield of isobuta'ne.

r actor. In run 2, about the same procedure and conditions were used exceptr that the hydrogen was replaced by nitrogen. At the end of the reaction period, the acid and the hydrocarbon The heavier or catalyst phase from separator i6 may be recycled through conduit 32 to reactor I2. Preferably, however, a suitable portion of it is passed through conduit 33to heater 34, wherein it is heated in the presence of hydrogen, admitted through inlet 35, to decompose organic iiuorine and organic boron compounds. The temperature in heater 34 may be in the range of about 100 or 200 to about 800 F.; preferably it is inthe range of about 350` to about 500 F. Although the catalyst may be regenerated in part by heating it in the absence of hydrogen, I have found that the regeneration' is much more nearly complete if a partial pressure of hydrogen in theJ range, for example, of about 100 to 500 p. s. i. is used. The eiliciency of regeneration may be still further increased by adding a minor proportion of a hydrogen carrier to the mixture prior to introduction into heater 34. The eiiluents from heater 34 pass through conduit 36 to flash chamber 31, wherein heavy carbonaceous materials or tar drop to the bottom as a semiliquid phase and are removed through outlet 38, and hydrogen, hydrogen fluoride, boron fluoride, and other volatile fluorine and boron compounds are flashed overhead and are passed through conduit 39 to distilling means ,40. Distilling means 40 eiects a nal separation by fractionation of regenerated hydrogen fluoride and boron fluoride from small proportions of oil,` tar, and the like carried over from flash chamber 31. Hydrogen and regenerated hydrogen fluoride and boron uoride are recycled from the top of distilling means 40 through conduit 4| to reactor I2, and oily material is withdrawn throughconduit 42. If desired, part of this oily material may be recycled through conduit 43 to heater 34 in order to recover additional hydrogen uoride and vboron fluoride. When hydrogen carriers are used it may be desirable in some instances to recover them from the tarwhich is withdrawn through outlet 38 by means such as are well known to those skilled in the art. For example,

.the tar may be oxidized to remove organic material and the resulting ash may be reconverted to the original salt by suitable chemical treatment.

To illustrate further some ofthe many aspects of the invention, the following specic examples are given.

Example I Two exploratory test runs were made to determine the influence of elementary hydrogen upon reconstruction'of hydrocarbons in the presence of concentrated hydroiluoric acid as a catalyst. In run 1 hydrofluoric acid was introduced A n-Heptane, gm.

Temperature, F

phases were withdrawn, separated, and examined. The following data were obtained.

Run No 1 2 Charge:

Hydroiluoric acid. lb 2. 18 2. 37 'drogeu pressure, p s i 1,000 N trogen pressure, p s i 1,000 Buteno-l, lb l. 38 06 Acid/olefin mol ratio. 4 0:1 8:2:1 Average Temperature, F.- 243 202 Total reaction period, min 215 1 Com sition o Product, wt.

ropane 0. 96 0. 2 Isobutane 34. 59 20. l n-Butane- 13. 61 4. 9 Pentanes 20.28 15.1 Heavier 30. 66 50. 7 .Acid-solubles in used acid, w oi used acid-. 21. 07 27.5

It appears from these data that the presence duction of a relativelycomplex product. However, it appears that by the use of a somewhat higher temperature and/or by adding a minor proportion of a hydrogen carrier, such as a halide of a metal of the group consisting of Cr, Sn, Cu, Ni, Co, Fe, Cd, Zn Mo, V, and Pb, to the reaction mixture a very high yield of isobutane may be obtained from the reconstruction of olens, in

the presence of hydroiluoric acid and hydrogen.4

Example II A 400 cc. steel vessel, which could be shaken on a rocker arm, was charged with n-heptane,A

HF, BF3, and hydrogen in the order given. Results are listed below.

Hydrogen, p. s. Time, mm

Composition of eilluonts,

per cent by weight:

Hydrogen Propane Isobutane n-Butane. Isopentane. n-Pentane Neohexane.. Diisopropyl 2- and S-methylpentane n-Hexane. Isoheptane.. 11-Heptane Octanes and heavier Hydrogen/carbon ratio v Eample III A steel vessel having a capacity of 350 cc. and

insure adequate mixing was charged with a parain hydrocarbon to/ be converted, hydrogen, hydroiiuoric acid, and boron trifluoride, in that order, in the amounts and with the results shown 10 6. A process for improving the activity of a partially spent liquid concentrated hydrouoric acid catalyst which has been used in the conversion of hydrocarbons and which has become conin the following table. taminated with organic impurities soluble there- Run No.. 5 6 7 8 9 1o 11 12 13 Wt. Wt. Wt. Wt. Wt. Wt. Wt. Wt t Gm Gm G Gm Gm Gm Gm Gm. Gm

Normal Hexane 2-Methy Pentane Normal Pentole 82 82 y82 n 82 65 65 76 76 vI7 0 100 25 27 0 240 0 53 1.085 30 90 33 10 18 20 20 30 30 Temperature, F.-." 178 178 176 176 129 140 165 167 176 Conversion of Parain, a... 88.8 Low 83.9 57. 7 88. 2 24. 4 Very low Composition of Eillucnt Hydrocarbon, Per cent by Weight:

Propane 2.54 1.55 0.38 1148 0.86 98% Isobutane. 25.16 Boiling 11.11 2.19 29.65 3 .2 31.60 o 94 Boiling Nbutane. 5. 23 from 0.92 0. 25 4. 94 5. 64 from Isopentane... 18. 37 149 15. 39 0. 65 19. 40 2. 30 20. 43 22. 07 91 N-pcntane 3.69 to l. 72 0.94 2. 37 11.80 75,56 to Ncohexane... 13. 26 158 F 15. 74 6. 23 8. 74 3.09 4. 56 104 F. Disopro 1. 40 indicating 1. 35 9. 21 1. 71 16. 16 1. 30 indicating Mcthylpentanes 8.63 very low 19.65 33. 46 10.13 71.87 11.00 l 43 very low -hexane 11. conversion 16. 14 42. 29 2. 74 conversion Isopentane 6. 9. 80 1.44 6. 92 2.12 6.08 N -heptane and heavier.. 4. 22 6. 63 2. 96 1I. 92 0. 74 6. 73

100. 0c 10o. 0o 10o. oo 10c. 0o i100. oo 100.00 10o. oo

This invention is broadly applicable to the 30 1n, which comprises subJecting such a spent cattreatment of aliphatic hydrocarbons, and is particularly valuable for treating normally liquid parafiins and/or oleiins. Many modiiications of this invention will be obvious to those skilled in the art. Hence, it is not intended that mention herein of specific apparatus, materials, conditions, or purposes should unduly limit the scope of my invention. In the speciiic embodiments described, it is understood that additional equipment such as pumps, valves, coolers, fractionators, or the like, such as are `well-known 'to those skilled. in the art, may be used wherever needed r convenient.

I claim:

1. A process for the production of isobutane from a low-boiling olefin having at least four carbon atoms per molecule, which comprises subjecting such an olefin hydrocarbon to conversion conditions in the presence of and intimately admixed with liquid concentrated hydroiluoric acid as the effective 'catalyst with a hydrocarbon to catalyst ratio in the range of about 0.1:1 to about 3:1 by weight and in the presence of free hydrogen under a pressure of at least 200 pounds per square inch.

2. The process cf claim-1 in which said lowboiling olen is a normal butene.

3. The 'process of claim 1 in which the catalyst comprises between about 0.1 and about 10 per cent by weight of boron triuoride.

4. The process of converting an olenic hydrocarbon material to a more highly saturated hydrocarbon material, which comprises subjecting an olenic hydrocarbon material to the action of a substantial amount of free hydrogen and in the presence of and intimately admixed with liquid concentrated hydrofl'uoric acid as the essential catalyst with a hydrocarbon to catalyst ratio in the range of about 0.1:1 to about 3:1 by weight under conversion conditions such thathydrocarbon effluents of said conversion are substantially lfree from olefin hydrocarbons.

5. The process of claim 4 inzwhich the catalyst comprises between about 0.1 and about 10 per cent by weight o i boron trlfiuoride. i

alyst to an elevated temperature not greater than about 800 F. in the presence of'free hydrogen under a partial pressure of at least pounds per square inch and in the ypresence of a halide of a. metal of the group consisting of chromium, tin, copper, nickel, cobalt, iron, cadmium, zinc, molybdenum, vanadium, and lead, for a time sufficient to effect a reaction of free hydrogen with said organic impurities, thereby effecting a puri,- cation of said liquid concentrated hydro'uoric acid catalyst.

'7. The process of claim 6 in which said treatment is conducted at a temperature between about 350 and about 500 F.

8. The process of claim 6 in which said metal halide is a halide of chromium.

9. The process of claim 6 in which said metal halide is a halide of vanadium.

10. The process of claim 6 in which said metal halide is a halide of molybdenum.

11. A process for the conversion of a lowboiling parafiin hydrocarbon having at least five and not more than seven carbon atoms per molecule to lower-boiling'parain hydrocarbons,

which comprises reacting such a hydrocarbon at a reaction temperature between about 100 and about 350 F. while intimately admixed with a liquid catalyst comprising concentrated hydroluoric acid as the essential catalyst and in the presence of a halide of a metal of the group consisting of chromium, tin, copper, nickel, cobalt, iron, cadmium, zinc, molybdenum, vanadium, and lead, with a hydrocarbon to catalyst ratio in the range of about 0.1:1 to about.3:1 by weight, and while associated with free hydrogen under a partial pressure between about 200 and about 5000 pounds per square inch for a time such as to effect a substantial extent of conversion of the paraiiin hydrocarbon so treated.

12. The process of claim 11 in which said metal halide is a halide of vanadium.

13. A process for the conversion of a lowboiling paraiiin hydrocarbon having atleast ve and not more than seven carbon atoms per molecule to lower-boiling paraiiin hydrocarbons,

l1 t which comprises reacting such a hydrocarbon at 'a reaction temperature between about 100 and 'about 350 F. while intimately admixed with a lower-boiling Praiiln hydrocarbons, which comwhile associated with free hydrogen under a parl tial pressure between about 200 and about 5000 pounds per square inch l for a time such as to eifect a substantial extent of conversion oi the paraiiln hydrocarbon so treated.

14. A process for the conversion of a lowboiling aliphatic hydrocarbon having atleast four carbon atoms per molecule to a different aliphatic hydrocarbon having a molecular weight not greater than the aliphatic hydrocarbon converted, which comprises subjecting such an aliphatic hydrocarbon to the catalytic action of .and intimately admixed with liquid concentrated hydrofiuoric acid and in the presence of a halide oi a metal of the group consisting of chromium, tin, copper. nickel, cobalt, iron, cadmium, zinc, molybdenum, vanadium, and lead, with a hydrocarbon to catalyst ratio in the range of about 0.1:1 to about 3:1 by weight under conversion conditions and in the presence oi.' a substantial yamount oi' free hydrogen.

15. The process of claim 14 in which said metal halide is a halide of vanadium.

16. The process of claim 14 in which the liquid catalyst also contains between about 0.1 and about per cent by weight of boron trifluoride.

17. A process for the conversion of a normal n butene to isobutane, which comprises subjecting a normal butene to conversion conditions in the presence of and intimately admixed with liquid concentrated hydroiluoric acid as the effective catalyst and in the presence of a halide of a metal of the group consisting or chromium, tin, copper, nickel, cobalt, iron, cadmium, zinc, molybdenum, vanadium. and lead, with a hydrocarbon to catalyst ratio in the range of about 0.1:1 to about 3:1 by weight and in the presence of free hydrogen under a partial pressure of at least 200 pounds per square inch.

18. A process for the conversion of a low-bolling olen to isobutane, which comprises sulnlecting a low-boiling oleiln having at least four carbon atoms per molecule to conversion conditions in the presence of and intimately admixed with liquid concentrated hydrofiuoric acid as the eiective catalyst and in the presence of a halide of a metal of the group consisting of chromium, tin, copper, nickel. cobalt, iron, cadmium, zinc, molybdenum, vanadium, and lead, with a hydrocarbon to catalyst ratio in the range of about 0.1 1 to about 3: 1 by weight and in the presence of free hydrogen under a partial pressure of at least 200 pounds per square inch.

,19. 'I'he process oi' claim 18 in which the liquid catalyst also contains .between about 0.1 and about10 per cent by weight of boron triuoride. t

20. A process for the conversion of at leastone paramn hydrocarbon having at least five and not more than seven carbon atoms per molecule to prises reacting sucha lparatiin hydrocarbon at a reaction temperature between about 100 v and about 350 F. while intimately admixed with4 a K catalyst selected from the groupffconsistlng of liquid concentrated hydrofluorlc acid, liquid concentrated hydroiluoric acid together with boron triiiuoride in an amount between about 0.1 and about 8 per cent by weight of the total catalyst, and each of theaforesaid catalysts together with a halide of a metal of the group consisting of chromium, tin,

with a hydrocarbon to catalyst ratio in thev range of about 0.1:1 to about 3:1 by Weight andl while v 5 minutes and about 2 hours and such as toeffect a substantial extent of conversion of the pjarain hydrocarbon so treated to produce lower-boiling parain hydrocarbons, and recovering fromr efiiuents of said reaction a paraffnic hydrocarbon fraction containing a paraflin hydrocarbon so produced and lower-'boiling than the paramn hydrocarbon reacted.

21. A process for the conversion ofa low-boiling aliphatic hydrocarbon having at least four and not more than seven carbon atoms per molecule to isobutane, which comprises reacting such an aliphatic hydrocarbon at a reactiontemperature between about and about 350 F. while intimately admixed with a catalyst selected from the group consisting of liquid concentrated hydrofiuoric acid, liquid concentrated hydroiluoric acid together with boron-triiluoride in an amount between about 0.1 and about 8 per cent'by weight of the total catalyst, and each of the aforesaid catalysts together witha halide of a metal oi the group consisting of chromium, tin, copper, nickel,

cobalt, iron, cadmium, zinc, molybdenum, vanadium, and lead, with a hydrocarbon to catalyst.

ratio in the range of about 0.1:1 to about 3:1 by weight andwwhile associated with free hydrogen under a partial pressure between about 200 and about 5000 pounds per square inch for a time between about 5 minutes and about 2 hours and such as to eii'ect a substantial extent of conversion of said aliphatic hydrocarbon to iso butane, and recovering from eilluents of said reaction a hydrocarbon fraction comprising. isobutane so produced.

. FREDERICK E. FREY.

REFERENCES CITED The following references are of record in the file of this patent:

UNITED STATES PATENTS copper, nickel, cobalt, iron,` cadmium, zinc, molybdenum, vanadium, and lead, 

